EP2146143A2 - Procédé et dispositif pour générer un gaz pauvre en azote ou dépourvu d'azote - Google Patents

Procédé et dispositif pour générer un gaz pauvre en azote ou dépourvu d'azote Download PDF

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Publication number
EP2146143A2
EP2146143A2 EP09450130A EP09450130A EP2146143A2 EP 2146143 A2 EP2146143 A2 EP 2146143A2 EP 09450130 A EP09450130 A EP 09450130A EP 09450130 A EP09450130 A EP 09450130A EP 2146143 A2 EP2146143 A2 EP 2146143A2
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EP
European Patent Office
Prior art keywords
zone
gasification
fluidized bed
gasification zone
bed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP09450130A
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German (de)
English (en)
Other versions
EP2146143A3 (fr
Inventor
Klaus Bosch
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Biomassekraftwerk Betriebs GmbH and KG
Original Assignee
Energie Oberwart Errichtungs GmbH
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Application filed by Energie Oberwart Errichtungs GmbH filed Critical Energie Oberwart Errichtungs GmbH
Publication of EP2146143A2 publication Critical patent/EP2146143A2/fr
Publication of EP2146143A3 publication Critical patent/EP2146143A3/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/06—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone the circulating movement being promoted by inducing differing degrees of fluidisation in different parts of the bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
    • C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/20—Inlets for fluidisation air, e.g. grids; Bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2206/00—Fluidised bed combustion
    • F23C2206/10—Circulating fluidised bed
    • F23C2206/101—Entrained or fast fluidised bed

Definitions

  • the present invention relates to a method for producing a nitrogen-poor or virtually nitrogen-free gas by gasification of heterogeneous, biogenic fuels or mixtures of heterogeneous, biogenic fuels and plastics, and to an apparatus for carrying out this method.
  • the US Pat. No. 3,853,498 discloses a process in which domestic waste is pyrolyzed in an inert atmosphere and the fuel is heated in a separate combustion zone.
  • the US 4 405 339 A proposes a fluidized bed apparatus comprising a zone for cracking fuel and a heating zone for heating the heat transfer medium by combustion of the residues from the cracking zone.
  • the processes of the latter two patents lead to a product gas containing a too high proportion of hydrocarbons for our purposes.
  • the EP 202 215 A2 discloses a combustion process in a fluidized bed furnace with internal circulation of the solid. However, no product gas is generated.
  • the GB 2 203 445 A proposes a process for the production of methane, in which the gasification takes place in a circulating fluidized bed.
  • the AT 405 937 describes a process wherein, to produce a nitrogen-lean, or nearly nitrogen-free gas by gasification of heterogeneous, biogenic fuels and plastics, the fuel to be gasified first brought into contact with the hot bed material of a fluidized bed combustion under exclusion of air and thereby at least in the presence of water vapor and / or CO2 Partially degassed. The resulting residual fuel is fed to a fluidized bed (2) with circulating bed material and thereby burned, whereby the bed material is heated and is returned after its separation from the exhaust gas back into the vestibule (1).
  • the gasification plant for implementation of the method is characterized in that it is formed in a housing of an internally circulating fluidized bed, wherein the antechamber (1) is used for the return of the hot bed material and is formed as a gasification chamber, while the actual fluidized bed (2) is formed as a combustion zone , wherein for the integration of the bed material in the fluidized bed (2) and in the return of the hot bed material in the vestibule (1) lock-like devices are provided.
  • the bed material is sand mixed with catalytically active nickel and / or niobium compounds, thereby lowering the gasification temperature and controlling the gas composition, especially in the direction of reducing the CH 4 content.
  • the in AT 405 937 B described method has the disadvantage that the automatically adjusting temperatures in the gasification and combustion part can not be practically influenced. In practice, this means that the process is almost unusable, since the temperature in the gasification for the gas quality and in particular for the tar content of the product gas is crucial. The possibility of regulating the temperature to a desired value is therefore absolutely necessary.
  • Object of the present invention is to overcome the disadvantages of To avoid prior art and to provide a method and an apparatus in which the temperatures in the gasification and combustion part can be influenced.
  • a reactor comprising a gasification zone and a combustion zone
  • the reactor has a fluidized bed material which is continuously heated Condition is passed from the combustion zone into the gasification zone and from the gasification zone in the cooled state together with non-gasified residual fuel back into the combustion zone, to introduce the fuel into the gasification zone formed as a circulating fluidized bed, wherein a part of the fluidized bed is designed as a moving bed, the fuel in The circulating fluidized bed of the gasification zone at Heilab gleich to form a product gas at least partially to degas or gas and the remaining or unreacted residual fuel together with the cooled bed material on the Wanderbe to spend in the combustion zone, where the bed material is fluidized to form a fast fluidized bed, reheated by combustion of the residual fuel, and recycled to the circulating fluidized bed of the gasification zone.
  • the present invention thus provides that a portion of the fuel to be gasified is introduced directly into the combustion part together with the circulating bed material.
  • This can be realized by appropriate design measures in the gasification part, wherein the lower part of the carburetor is changed so that by suitable combination of the feed point and the fluidization, the amount of fuel flowing into the combustion chamber, can be influenced.
  • Fluidization in two levels e.g., as a two-stage supply of gasification agent
  • the circulating fluidized bed in the gasification zone of the reactor is provided by different fluidization rates over the cross section of the gasification zone of the reactor.
  • the product gas is freed from dust formed in the gasification zone, the dust being transported as additional fuel via the moving bed into the combustion zone.
  • the particle discharge from the gasification section has proven to be a major shortcoming. Even with normal wood chips, the fine fraction had to be partially screened out in order to be able to control the higher tar load associated with higher fines.
  • the problem is the too short residence time of the small fuel particles in the hot carburetor area.
  • the present invention provides an internal particle separator, whereby the fine particles thus remain in the hot gasification section and can be gasified there regularly without producing higher amounts of tar.
  • the non-gasified dust material is then used as additional fuel and spent on the moving bed in the combustion zone.
  • the formation of the above-described circulating fluidized bed in the gasification section can be useful by the deposited and tends to float dust is introduced specifically into the downward circulation flow. In this way, it is transported together with not yet gassed fuel to the transition and finally into the combustion zone. This also ensures that fine ash, which can be discharged only via the combustion part, also gets there.
  • the present invention furthermore relates to a device for producing a nitrogen-poor or virtually nitrogen-free gas by gasification of heterogeneous, biogenic fuels, residues and / or plastics in a reactor a gasification zone and a combustion zone, wherein the reactor has a bed material fluidized by inflow of fluidizing gas via feed lines, which in the heated state via a line continuously from the combustion zone into the gasification zone and in the cooled state via a line from the gasification zone together with non-gasified residual fuel is conducted into the combustion zone, characterized in that the fuel is introduced via a line in the formed as a circulating fluidized bed gasification zone, wherein a part of the fluidized bed is designed as a moving bed, the fuel in the circulating fluidized bed of the gasification zone at Lucasab gleich to form a product gas at least is partly gasified or gasified and the remaining or unreacted residual fuel is spent together with the cooled bed material on the moving bed and via the line in the combustion zone, where the Bed material fluidized to form a fast
  • the circulating fluidized bed is provided in the gasification zone of the reactor by means of suitable internals, such as baffles.
  • suitable internals such as baffles.
  • inlet nozzles for fluidizing gas are provided in the bottom region of the gasification zone of the reactor in the vicinity of the fuel feed and / or in the environment or in the line from the gasification zone into the combustion zone for the purpose of providing the moving bed.
  • the adequate circulation of the bed material is an essential part of the functionality of the process.
  • the transfer of the bed material from the gasification zone in the combustion zone is often done in practice via an inclined fluidized slide (here, the inclination angle of the slide is crucial), this is often a weak point in terms of material flow but also leakage of air into the gasification zone, which largely avoided must become.
  • the inlet nozzles by the impulse of the incoming gas actively supports the flow of solids from the gasifier zone into the combustion zone and counteracts the leakage, both requirements can be met much better.
  • a device is also provided in which the gasification zone of the reactor has on the outlet side devices for the separation of dust formed in the gasification zone, the separated dust being transported via a guiding device in the inside of the gasification zone into the circulating fluidized bed or into the moving bed.
  • the devices for separating dust formed in the gasification zone are selected from the group consisting of filtering separators, centrifugal separators and combinations thereof, and if metal or ceramic candle filters are used as filtering separators, which may be used for the Teerspaltung catalytically active materials are populated.
  • the internal separators may, as stated, be made differently and may, for example, operate on a centrifugal basis (e.g., cyclones) or as filtering separators (e.g., metallic or ceramic candle filters).
  • it is advisable to use catalytically active materials for the tar splitting which enables a significant tea reduction at suitable temperatures.
  • a combined particle and tar separation would be possible and it can downstream devices avoided and also the product gas can be cooled easily without having to fear a tar condensation.
  • Sand or catalytically active natural materials preferably calcite, dolomite or olivine or mixtures thereof may be used as the bed material.
  • nickel and / or zirconium compounds come into question.
  • FIG. 1 shows a schematic cross section through an inventive design of a carburettor with internally circulating fluidized bed in the gasification section, moving bed and faster Fluidized bed in the combustion part and in addition an internal dust separation with return of the dust into the moving bed.
  • Fig. 2 is a schematic cross section of an embodiment of a carburetor according to the invention shown with internally circulating fluidized bed in the gasification section and combined fuel-dust return to the chute and faster fluidized bed in the combustion part.
  • FIGS. 3a and 3b show examples of inventive embodiments of the flow in the transition from the gasification in the combustion part or optionally in the moving bed ( FIG. 3a Hole bottom design in basic and elevation,
  • Fig. 3b Nozzle for nozzle bottom design in basic and elevation).
  • the gasification reactor according to Fig. 1 consists of a circulating fluidized bed (1) in the gasification region, a moving bed (2), in which the fuel is introduced, a connecting line (3) (here designed as a connection slide) between the gasification zone and formed as a fast fluidized bed combustion zone (4) and a another connecting line (5) with cyclone and siphon for the return of heated bed material in the gasification zone.
  • the fuel supply (6) takes place in the moving bed (2), which can be adjusted by suitable fluidization of the fuel input into the connecting chute (3).
  • the fluidization of the gasification fluidized bed (1) is divided and can therefore be set differently.
  • a circulation of the bed material sets in a clockwise direction.
  • particles which tend to float are carried downwards and can thus be transported via the connecting chute (3) and further into the combustion zone (4).
  • internals eg baffles (14)
  • the gas supply can be adjusted independently of each other, that the desired circulation of bed material between the gasification zone (1) and combustion zone (4) results.
  • a particle separator (15) is shown according to the invention, for example a cartridge filter with pulse cleaning.
  • This particle separator (15) By means of this particle separator (15), a dust-free and tarry raw gas can be achieved even at higher fines in the fuel.
  • the separated particles are introduced via a collecting line (16) directly into the connecting chute (3) and thus transferred into the combustion zone (4). This prevents unwanted accumulation of fine ash particles in the gasification zone.
  • the fine particles are burned out and leave the reactor via the cyclone of the combustion zone as fly ash.
  • FIG. 2 is another possible embodiment of the gasification reactor of the invention shown schematically.
  • the fuel supply (6) in the upward flow of solids of the circulating fluidized bed (1).
  • the fuel to be gasified is transported upwards, partially gassed, but when arrived at the top, it is at least partially flushed into the moving moving bed (2) and transported down there, and flows into the connecting chute (3).
  • the moving bed (2) is simultaneously used to transport the fine particle stream coming from the internal separator (15) into the connecting chute (3) and further into the combustion zone (4).
  • FIG. 3 shows inventive embodiments of inlet or inflow devices (13) of the embodiments according to Fig. 1 or 2 for the chute (3) or optionally also for the moving bed (2).
  • Fig. 3a shows a section of a perforated bottom
  • Fig. 3b a nozzle for a nozzle bottom. Both have in common that the gas flowing into the reactor exerts an impulse on the bed material in its flow direction (traveling direction), which results in advantages for the circulation of the solids and in the reduction of leaks.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Dispersion Chemistry (AREA)
  • Materials Engineering (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Gasification And Melting Of Waste (AREA)
EP09450130.1A 2008-07-16 2009-07-16 Procédé et dispositif pour générer un gaz pauvre en azote ou dépourvu d'azote Withdrawn EP2146143A3 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
ATA1106/2008A AT507176B1 (de) 2008-07-16 2008-07-16 Verfahren und vorrichtung zur erzeugung eines stickstoffarmen bzw. nahezu stickstofffreien gases

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Publication Number Publication Date
EP2146143A2 true EP2146143A2 (fr) 2010-01-20
EP2146143A3 EP2146143A3 (fr) 2014-03-05

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2639289A1 (fr) * 2012-03-16 2013-09-18 Spanner RE² GmbH Dispositif de génération d'un mélange de gaz combustible
CN108167824A (zh) * 2017-12-27 2018-06-15 宁波联创同宇环保科技有限公司 一种循环流化床电站锅炉系统
CN108546570A (zh) * 2018-05-30 2018-09-18 华中科技大学 一种基于循环流化床的返料脱炭一体化装置
CN109852431A (zh) * 2019-03-06 2019-06-07 中聚信海洋工程装备有限公司 一种循环流化双床热煤气站及其制气工艺
CN110511787A (zh) * 2019-09-21 2019-11-29 贵州丝域环能科技有限公司 一种新型有机固体废弃物制氢双流化床装置
CN112013381A (zh) * 2020-09-01 2020-12-01 中国科学院工程热物理研究所 一种耦合双流化床低氮燃烧装置及方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3853498A (en) 1972-06-28 1974-12-10 R Bailie Production of high energy fuel gas from municipal wastes
US4405339A (en) 1980-08-07 1983-09-20 Mittetu Chemical Engineering, Ltd. Process and apparatus for gasifying combustible materials
EP0202215A2 (fr) 1985-04-30 1986-11-20 Simmering-Graz-Pauker Aktiengesellschaft Procédé et dispositif de combustion des combustibles solides, liquides, gazeux ou pâteux dans un four à lit fluidisé
GB2203445A (en) 1987-04-16 1988-10-19 British Gas Plc Gasifying carbonaceous material
EP0302849A1 (fr) 1987-07-21 1989-02-08 SGP-VA Energie- und Umwelttechnik Gesellschaft m.b.H. Procédé et dispositif de combustion ou de gazéification des combustibles dans un lit fluidisé
AT405937B (de) 1995-11-03 1999-12-27 Austrian Energy & Environment Verfahren zur erzeugung eines stickstoffarmen gases und vergasungsanlage

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CN108546570A (zh) * 2018-05-30 2018-09-18 华中科技大学 一种基于循环流化床的返料脱炭一体化装置
CN108546570B (zh) * 2018-05-30 2024-05-14 华中科技大学 一种基于循环流化床的返料脱炭一体化装置
CN109852431A (zh) * 2019-03-06 2019-06-07 中聚信海洋工程装备有限公司 一种循环流化双床热煤气站及其制气工艺
CN109852431B (zh) * 2019-03-06 2020-11-06 中聚信海洋工程装备有限公司 一种循环流化双床热煤气站及其制气工艺
CN110511787A (zh) * 2019-09-21 2019-11-29 贵州丝域环能科技有限公司 一种新型有机固体废弃物制氢双流化床装置
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